Process for refining cracked gasoline



Dec. 24, 1935. J. c. BLACK PROCESS FOR REFINING CRACKED GASOLINE Filed Nov. 9, 1926 2 Sheets-Sheet l CECE! :CCEC

INVENTOR ATTORNEY Dec.24, 1935. 'J A 2,025,409

PROCESS FOR REFI NING CRACKED GASOLINE Patented Dec. 24, 1935 UNITED STATES PATENT OFFICE PROCESS FOR REFINING CRACKED GASOLINE Application November 9, 1926, Serial No. 147,294

9 Claims.

The invention of this application pertains to a process and apparatus for refining gasoline.

l have found that the impurities in crude gasolines, which impurities must be refined out before the gasoline is marketable, concentrate in the heavier boiling fractions of the gasoline in'the distillation of the gasoline. Thus the first 20% of a gasoline requires considerably less refining in proportion than does the last 80% of a gasoline. I have found that the refining of a gasoline in the usual methods, that is by treatment with sulphuric acid, alkali, whether hot or cold treatment, with clays, hypochlorites, distillations, etc., entails losses of the volatile ends of the gasoline, and so raises the initialboiling points of the gasoline.

The object of this invention is to prevent this loss of light volatile products by repeated handling and processing, and to so conserve the initial boiling points of the gasoline and the yield. I have also found that. by separating the light fraction from the heavierv fraction the total amount of treating reagent required is considerably reduced. This is due to the fact that a more accurate proportioning of the amount of reagent which each fraction requires is made possible by the separation of the fractions. The above considerations apply with particular force to cracked gasoline, since these cracked gasolines require a more rigorous treatment to purify them. Much more acid and alkali is required and more doctor solution and hypochlorite is required. This means that the loss of light fractions and the savings entailed by the separation from the light fraction and the heavier. fraction before treatment is magnified. i

The process will be better understood with reference to the accompanying drawings which show a schematic layout of the apparatus required for carrying out my invention. Figure l is a schematic outline of an apparatus required for the treatment of the gasoline according to the process of this application. Figure 2 is a. schematic outline of a modified treatment of the several fractions.

2 are trays located in evaporator 3.

bubble tower 6 with bubble tower 24. I is a valved residuum drawoflf from evaporator 3. II is a liquid trap for removing liquid condensate collected in tower 6. I2 is an evaporator to which trap ll connects. l3 are steam coils in said evaporator. I4 is a vapor line for removing" vapors generated in chamber l2. I5 is a condenser connected with said vapor line. I6 is a lookbox situated in condensate run down line. I! is a vapor vent for said lookbox. i1 is a condensate tankfor collecting condensate passing from lookbox l6. I8 is a line connecting tank I1 and the upper trays of bubble tower 6. I8 is a valve in said line. I9 is a pump in said line. is a condensate drawofi for separating un- 15 vaporized residuum from evaporator l2. 2| is a cooler in said line. 221s a tank connected to said drawoif. I are bubble trays in the aforementioned bubble tower 24. 26 is an analyzer connected in the top of said bubble tower. 21 is a vapor line connecting the top of said bubble tower to condenser 30. 29 is a line connecting tank 35' with analyzer 26. 29' and 29" are valves in said line. 29' is a valved bypass connecting line 29 with bubble tower 24. 25' connects analyzer 26 with the trays 25, bubble tower 24. 36' is a pump in line 29. 3| is a lookbox in condensate run down line which connects condenser 30 with tank 33. 34 is a line connecting condensate tank 33 with pump 35. 36 is a line connecting pump with blending tank 31.

is aided by coils 4i and the rectification aided by analyzer 48. at is a vapor line connecting the top of still 46 with condenser 50. 5i is a vented lookbox in condensate run down line, which connects condenser 56 with tank 52. 53 is a line connecting tank 52 with blending tank 31. 54 is a pump in said line. 55 is a line removing the stripped absorption oil from-the bottom of still 46. Said line connects to heat exchanger 42. 56-is a line connecting exchanger 42 with cooler 58. 56. is a valve in said line. 51 is a pump in said line. 39 is the aforementioned line, connecting cooler 58. with absorption tower 38.

59 is a line connectingtank 35 with the treating unit for the heavy ends of the cracked gaso- 55 pump is connected to alkali tank I49.

line removed from bubble tower 24. 60 is a pump in line 59. ing mixer, to the bottom of which are connected line 59 and line 63. Line 63 connects via pump 64 with acid tank 65. 61 is a separator. Line 66 connects treater 62 with separator 61. 68, controlled by valve 68, is an acid sludge draw-01f from separator 61. 69 is a line connecting separator 61 with alkali treater 10. To the bottom of said alakali treater is connected alkali tank 13 by means of line H and pump 12. 15 is a separator, to which is connected treater 18 by means of line 14. 16, controlled by valve 16, is an alkali drawofi from separator 15. 11 is a line for removing the gasoline from 15.

19 is a still, to which is connected line 11. 18 are bubble trays in said still. 18 is an analyzer in said still. are steam coils in said still. 8| is a residuum drawofi in which is pump 82 and cooler 83. 84 is a line connecting cooler 83 with tank 22. is a vapor line connecting the top of still 19 with condenser 86. 81 is a lookbox in condensate run down line 89. 88 is a. vapor vent connected with said lookbox. is a condensate tank connected to line 89. 9I is a line connecting tank 90 with pump 92. 93 is a line connecting pump 92 with tank 31.

94 is a line connecting the blending tank 31 with a treating unit. In this line is pump 95. 96 is an acid treating agitator, to which is connected line 94 and line 98, which line connects with acid tank 91 and has in it pump 99. I08 is a line for connecting the treater '96 with separator IOI. I02, controlled by valve I02, is an acid drawofi from the separator. I 03 is a gasoline drawoif from the separator connected to alkali treater I04. The bottom of I04 is connected to alkali tank I05 by means of line I06 and pump I81. I08 connects the alkali treater I04 with separator I09, to which separator is connected alkali drawoff IIO, controlled by valve II8. Gasoline draw off line II I connects separator I09 with the hypochlorite treater II2, to which is connected hypochlorite tank II3 by means of line H5 and pump II4. Separator I I1 is connected to treater I I2 by means of line H6. H8, controlled by valve H8, is a hypochlorite drawofi from separator H1. H9 is a gasoline drawofi from separator I I1 to finished gasoline tank I20.

Figure 2 shows a modification for treating various fractions separated thus: The gasoline from tank 52 of Figure 1 and tank 33 of Figure 1 are blended by means of pump I2I, line I22, pump I24, line I25 and tank I23. I26 is a pump in line I 21, connecting the tank I23 with the treater I28. I29 is a diluted alkali tank which is connected to treater I28 by means 01' line I3I and pump I30. I32 is a line connecting treater I28.with separator I33. I34 is a valved drawofi line connected to separator I33. I35 is a line connecting separator I33 with alkali treater I39. I36 is an alkali tank. I38 is a line connecting alkali tank I36 with treater I39. I31 is a pump in said line. MI is a separator. which is connected to treater I39 by line I48. I42 is a line connecting separator I4I with tank I29. I43 is a pump in said line. I44 is a line connecting separator I4I with tank I45. I44 is a valve in said line. I46 is a pump in said line.

I 41 is a line for introducing the acid treated heavy gasoline from treater 62 and separator 61 of Figure 1 into alkali treater I48. To I48 is connected line I5I, in which is pump I50, which I52 connects the alkali treater with separator I53. To

62 shows schematically an acid treat- I19 with pump I81.

the separator is connected valve alkali drawoif I54. I55 connects separator I53 with alkali treater I56. To this alkali treater is connected alkali tank I51 by means of line I58 and pump I59. I60 connects treater I56 with separator I6I. I62 is 5 a line connecting separator I6I with tank I49. I63 is a pump in said line. I64, in which there is a valve I64, connects the separator I6I with tank I66. I65 is a pump in said line. I61 is a crude oil tank. I68 is a line connecting tank 10 I61 with tank I66. I68 is a valve in said line.

I 69 is a pump in said line. I10 is a line connecting tank I66 with still I12. I10 is a valve in said line. I1I is a pump in said line. I14 is an analyzer in said still. I13 are steam coils in said 15 still. I15 is a vapor line connecting said still with condenser I16. I11 is alookbox situated in condensate run down line I18, which connects condenser I16 with tank I19. I80 is a line connecting tank I45 with tank I84. I8I is a pump in 20 said line. I82 is a bypass line connectihgline I80 with still I12. I82 is a valve in said liner I80 is a valve in line I 80. I83 is a line connecting tank I19 with tank I84. I84 is a pump in said line and I83 is a valvein said line. I85 is a line 25 connecting tank I84 with pump I81. valve in said line. I86 is a line connecting tank I86 is a valve in said line. I88 is a line connecting line I18 with heater I90 in furnace I89. I9I is a line connecting" I90 with 30 still I12. I9I is a valve in said line.

The operation of this process is as follows:

The cracked gasoline vapor formed in any manner, as for instance by the evaporation of the cracked oil, expanded through valve I and 35 spread on pans 2, the vapors from which rise through plates 4.where they are scrubbed of any heavy fractions, rise through riser 5 and are fractionated in tower 6. The heavy ends of these fractions, which consist of uncracked oils 40 and heavy ends of the gasoline, are passed into chamber I2 where they are redistilled by the aid of steam from coils I3, and the heat of the vapors rising through riser 5. The vaporous fraction, consisting of the heavy ends of the gasoline 45 fraction and some gas oil, passes through line I4, is condensed in condenser I5, collected through lookbox I6 in tank I1. This condensate is picked up by pump I9 and pumped into line I8, into bubble trays I where it is redistilled, acting as a 50 reflux. The gasoline portion of the condensate passing in through I8 is vaporized and the gas oil fraction passes down and is collected in 6. The unvaporized fraction from I2, which consists of gas oil, is passed down through line 20 into 55 cooler 2I and is collected in tank 22. This fractionmay be used as a recycle oil in the crack ing process together with make up oil, or in any other manner desired. The crude gasoline passes out through line 9 and passes into the 6 fractionating tower 24 where it is. fractionated by aid of liquid passing through the analyzer 26, and injected into tower 24, and passing over the plates 25. The condensate formed and collected in 24 consists of the heavy ends of the gasoline 65 fraction. This may 'be further stripped by steam introduced into the bottom of tower 24 through steam coils 32. The overhead passing through 21 consists of the light ends of the gasoline fraction and includes, of course, extremely light and 70 gaseous constituents undesired in the final gasoline product. The percent of overhead through 21 can be regulated to any desired amount by the correct control of the fractionating equipment.

I85 is a lected in 24 are removed through line 33 and valve 33", cooled by cooler 34 and collected in tank 35, pumped via pump 36' through line 29, as previously stated. The amount of oil passing through analyzer 26 is regulated by bypass 29".

The gasoline is constantly removed by pump 60 through line 59 and separately treated. This mentioned the mixture of absorption gasoline and treatment may consist of any conventional type of treatment with acid and alkali, etc or may be ahot alkali treatment as described in Patent 1,592,329.

As described in Figure 1, this treatment consists of an initial acid treat. pumped by pump 60 into mixer 62 where. it meets acid from tank 65, which is pumped by pump 64, line 63, into mixer 62. The acid treated gasoline is then pumped through line 66 into separator 61. The acid sludge and excess acid are removed through line 68 and the acid treated gasoline passes through line 69 into the alkali treater 10, where it meets an alkali wash, alkali being taken from tank 13 by pump 12, line 1|. An intermediate water wash may be employed if desired. The thus treated gasoline is passed to a separator where the excess alkali is removed through connection 16, and the alkali treated gasoline passed through line 11 to still 19. In still 19 the gasoline is steam stilled and the overhead iscollected via line 85,- cooler 86, in .tank 90. The heavy ends which are unvaporized are removed from 'the still via line 8I, cooler; 83, and passed to tank 22 to mix with the oil removed from evaporator I2. The condensate collected in tank 90 is the refined heavy ends of the gasoline. The light fraction issuing through line 21 is condensed in 30 and collected in 33. The uncondensed gases pass, together with the uncondensed fractions from all the lookboxes, into scrubber 38 where they are washedby a conventional absorption system, as for instance in absorber 38 where they are washed by oil introduced through 39 over plates 40. The charged oil is passed through .heat exchanger 42 via heater 43 through line 44 and pump 45 into still 46 where it is distilled by aid of steam introduced via coils 41 and rectified by use of analyzer 48. The unvaporized oil, which consists of the original wash oil, is removed through exchanger 42, line 56 and cooler 58, by means of pump 51, and sent to absorber 38 where it passes over the bubble trays 40. The vapor passes through line 49, condenser 50, where it is condensed and the condensate collected in tank 52.

This condensate. is absorption gasoline and consists of the very light fraction of the gasoline.

:Ihis gasoline is blended with the other fractions in tank 31 in the correct proportion. As in other absorbers of conventional type the uncondensable gases leave the tower 38 through a vent or line This blended gasoline is still doctor sour, i. e. will give a positive result by the Wellknown do'ctor test, and in order to make it sweet it is given a final chemical treatment. For instance,

The gasoline is alkali pumped through I42 into tank I29.

from the gasoline in separator I09. The sepa rated gasoline is then pumped into treater II2 where it is treated with sodium hypochlorite pumped from-tank II3 through line II5, pump H4. The gasoline is separated from the excess hypochlorite in separator H1 and the finished doctor sweet gasoline collected in tank I20.

Instead of treating the fractions as above light gasoline cut may be treated together and then mixed with the treated heavy ends. For

' instance the absorption gasoline in tank 52 and the light cut in tank 33 may be blended in tank- I23, and the blended light gasoline cuts treat-' ed as described in the aforementioned Patent 1,592,329.

The gasoline is first acid treated, and the acid treated gasoline is then passed to treater I28 where it is mixed with diluted alkali from tank I29, and the excess acid neutralized. The alkali is separated from the gasoline in separator I33 and given a treatment with concentrated alkali at an elevated temperature under pressure in treater I39. The gasoline is separated from the alkali in MI and the diluted The treated gasoline is collected in tank I45. The heavy gasoline which has been acid treated is passed through a similar treatment where it is first given a diluted alkali wash in I48 by means of alkali pumped from I49, and the alkali. separated in separator I53. The gasoline is then given a treatment with more concentrated alkali at an elevated temperature in tank I56 by heating the mixture of alkali and gasoline under pressure. The gasoline is separated from the alkali in IN and diluted alkali pumped via line I 62 into tank I49. The treated gasoline is pumped via I64 into tank I66 where it is mixed with crude oil from I61. The mixture is then pumped Via line I10, heater I90, and distilled in still I12. Instead of mixing it with crude oil the gasoline may itself be steam stilled in still I 12 by by-passing the heater I90. The gasoline from tank I may be pumped into still I12 to act both as a wash oil and to obtain a blended gasoline. The overhead passes through line I15.

In operating without this vapor phase blending the gasoline is condensed in I16 and collected in I19 and blended with the gasoline from I45 in tank I84. The blended gasoline is removed through line I85and pump I81, valve I86 being closed, and pumped to final chemical treatment as in the previous case, in the instance of the gasoline pumped from the blended gasoline tank 31.

If the blending has been made in the vapor phase the blended gasoline in I19 is removed via pump I81 by closing valve I85 and I83 and w opening valve I 88, and the blended gasoline is then given the final chemical treatment as previously indicated.

Instead of giving the absorption gasoline and the light gasoline fraction an acid and a hot alkali treatment, the blended fractions may be merely washed with concentrated alkali at ordinary temperatures. I have found this sufficient preliminary treatment.

As a specific example of the treatment the following may be given as an illustration. A cracked gasoline generated via line 9 is fractionated in fractionating tower 24 so as to obtain approximately 30% overhead and 70% of condensed fractions. This 30% is condensed to produce 20% of light gasoline cut, which is blended with 7 the absorption gasoline, which corresponds usually to 10% of the total gasoline issuing through 9. The heavy end which is removed through 33' is treated as usual with acid and alkali, and the final blended product in 31 is given a lightacid treat with about 1%# of acid to the barrel of gasoline, and the usual treatment with alkali and hypochlorite or plumbite to make the gasoline doctor sweet, 1. e. so it shows a negative result by the well known test with doctor solution. By so operating it will be found that there has been a marked conservation of light products by showing a lower-end point and increased yield.

If the process as indicated by Figure 2 is employed the blended light gasoline cut and absorption gasoline is treated with acid, then with diluted alkali, and with more concentrated alkali at an elevated temperature of about 200 F. and

about 50# pressure, by either preheating the,

gasoline and alkali before introduction into treater I39, or by use of steam in the treater I39. The separated gasoline is blended as previously indicated. The heavy gasoline cut is treated in a similar manner and distilled and blended as indicated above. This treatment by hot alkali shows a marked reduction in the sulphur content, and also in the gum forming constituents 'of the gasoline.

Instead of treating the gasoline with hot alkali as here indicated the treatment with hot doctor solution is found very effective.

If a cold alkali treatment is used for the light gasoline cut and the absorption gasoline they may be treated in the cold with concentrated alkali and blended as above.

The gasoline I treat is'generally designated as naptha, in oil refinery terminology. Naptha is the name givento an untreated or impure gasoline stock. Therefore, in order to more ac curately set forth my invention, I have used the term naptha in the appended claims.

The above is not to be taken as limiting my invention but merely as illustrative of the best manner. of carrying out my invention, which I claim tobe:

l. The process of preparing marketable products from a mixture of hydrocarbons consisting chiefly of compounds of the gasoline range,.

which comprises subjecting the mixture in vapor form to partial condensation to produce a first condensate requiring chemical treatment and a second vapor whichrequires no chemical treatment and which represents at least 20% of the said mixture being treated, separating the second vapor into liquid products substantially free of normally gaseous hydrocarbons and into a gas. chemically treating the first condensate while it is in substantially the same condition it was in when separated in said partial condensation operation, and blending the treated condensate with the liquid products separated from the second, vapor.

2., The process-oi preparing marketable products from a -mixture of hydrocarbons'consisting chiefly of compounds of; the gasoline range, which comprises subjecting the mixture invapor form to partial condensation to produce a first condensate requiring chemical treatment and a second vapor which requires no chemical treat= merit and which represents at least 20% of the said mixture being treated, separating the second it is in substantially the same condition; it was Y in when separated in said partial condensation operation, blending the treated condensate with the liquid products separated from .the second" vapor and thereafter subjecting the blended .of the said mixture being treated,.separ'ating the second vapor into liquid products substantially free of normally gaseous hydrocarbons and into a gas, chemically treating the first condensate and blending the treated condensate with the liquid products separated from the second vapor after separation therefrom of said normally gaseous hydrocarbons;

4. The process of preparing marketable products from a mixture of hydrocarbons consisting 'chiefiy of compounds of the gasoline range, which comprises subjecting the mixture in vapor form to partial condensation to produce a first condensate requiring chemical treatment and a second vapor which requires substantially no chemical treatment and which represents at least 20% of the said mixture being treated, separating the second vapor into liquid products substantially free of normally gaseous hydrocarbons and into a gas, chemicallytreating the first condensate, blending the treated condensate with the liquid products separated from the second vapor after separation therefrom of said normally gaseous hydrocarbons and thereafter subjecting the blended product to a sweetening treatment.v

5. The method of treating the vaporous and gaseous mixture produced in the cracking of hydrocarbon oils, which comprises dephlegmating the mixture of vapors and gases to condense and separate therefrom constituents heavier than gasoline, subjecting gasoiine and normally gaseous constituents thereby freed from constituents heavierthan gasoline to rectification at a separate therefrom in liquid form a heavy gasoline cut while withdrawing in vapor form from said rectification stage a fraction containing at least 20% of the total desired gasoline product, and separating desiredlight gasoline constituents from normally gaseous constituents contained in the fraction withdrawn in vapor form from said rectifying stage, theseparation ofat least the lightest gasoline constituents being effected in a stage wherein a..hydrocarbon absorbent oil passes countercurrent to vapors and exerts a selective action thereupon and in the absence of the previously separated heavy gasoline cut.

6. The process of recovering refined gasoline from a mixture of hydrocarbons consisting chiefly of compounds of the gasoline range and normally gaseous hydrocarbons, which comprises subjecting the mixture to rectification at a temperature substantialiy above atmospheric to produce a first fraction comprising heavy gasoline requiring refining and a second fraction containing gasoline constituents which do not require drastic refining and which comprise at least 20% of the desired gasoline constituents in the de-.

phlegmated. vapors, separating the second fraction into liquid products comprising light gaso= line substantially free from normally gaseous hyliquid products separated from the second frac-' tion.

7. The process of recovering refined gasoline from a mixture of hydrocarbons consisting chiefly of compounds of the gasoline range and normally gaseous hydrocarbons, which comprises subjecting the mixture to rectification at a temperature substantially above atmospheric to produce a first fraction comprising heavy gasoline requiring drastic chemical refining and a second fraction containing gasoline constituents which do not require drastic chemical treatment and which comprises at least 20% of the desired gasoline constituents in the dephlegmated vapors, separating the second fraction into liquid products comprising light gasoline substantially free from normally gaseous hydrocarbons and into a gas, the separation of at least the lightest gasoline constituents being efiected in a stage wherein a hydrocarbon absorbent oil passes countercurrent to vapors and exerts a selective action thereupon and in the absence of the previously separated heavy gasoline fraction, chemically refining said heavy gasoline fraction and blending the treated heavy gasoline with the liquid products separated from the second fraction.

8. The process of recovering refined gasoline from a mixtureof hydrocarbons consisting chiefly of compounds of the gasoline range and normally gaseous hydrocarbons, which comprises subjecting the mixture to rectification at a temperaturc substantially above atmospheric to pro.-

duce a first fraction comprising heavy gasoline requiring refining and a second fraction containing gasoline constituents which do not require drastic chemical treatment and which comprise at least 20% of the desired gasoline constituents 5 in the dephlegmatedvapors, separating the second fraction into liquid products substantially free from normally gaseous hydrocarbons and into a gas in the absence of said heavy gasoline fraction, subjecting said heavy gasoline fraction 10 to a chemical treatment and a redistillation to remove undesired impurities therefrom, and blending the thereby refined heavy gasoline with liquid products separated from the second fraction. 15 9. The process of recovering refined gasoline from a mixture of hydrocarbons consisting chiefly of compounds of the gasoline range and normally gaseous hydrocarbons, which comprises subjecting the mixture to rectification at a tem- 2o perature substantially above atmospheric to produce a first fraction comprising heavy gasoline requiring drastic chemical treatment and a second fraction containing gasoline constituents which do not require drastic chemical treatment and which comprise at least 20% of the desired gasoline constituents in the dephlegmated vapors, separating the second fraction into liquid products substantially free from normally gaseous hydrocarbons and into a gas, in the absence of said heavy gasoline fraction, subjecting said heavy gasoline fraction to a relatively drastic chemical treatment and a re-distillation to remove undesired constituents therefrom, subjecting liquid products separated from the second fraction to a relatively mild chemical treatment, and blending the thereby refined heavy gasoline with the thereby refined liquid products separated from the second fraction.

JOHN 0. BLACK. 40 

